CN101845328B - Biomass combined gasification equipment - Google Patents
Biomass combined gasification equipment Download PDFInfo
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- CN101845328B CN101845328B CN2010101879126A CN201010187912A CN101845328B CN 101845328 B CN101845328 B CN 101845328B CN 2010101879126 A CN2010101879126 A CN 2010101879126A CN 201010187912 A CN201010187912 A CN 201010187912A CN 101845328 B CN101845328 B CN 101845328B
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- 238000002309 gasification Methods 0.000 title claims abstract description 83
- 239000002028 Biomass Substances 0.000 title claims abstract description 52
- 239000007789 gas Substances 0.000 claims abstract description 60
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 22
- 238000000197 pyrolysis Methods 0.000 claims abstract description 16
- 239000002245 particle Substances 0.000 claims abstract description 13
- 238000005336 cracking Methods 0.000 claims abstract description 12
- 239000007787 solid Substances 0.000 claims abstract description 12
- 239000000571 coke Substances 0.000 claims description 22
- 238000006243 chemical reaction Methods 0.000 claims description 21
- 239000000567 combustion gas Substances 0.000 claims description 21
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 12
- 238000002485 combustion reaction Methods 0.000 claims description 12
- 229910052760 oxygen Inorganic materials 0.000 claims description 12
- 239000001301 oxygen Substances 0.000 claims description 12
- 239000011285 coke tar Substances 0.000 claims description 9
- 239000002131 composite material Substances 0.000 claims description 8
- 238000000926 separation method Methods 0.000 claims description 8
- 239000000126 substance Substances 0.000 claims description 8
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- 238000010517 secondary reaction Methods 0.000 claims description 7
- 239000003570 air Substances 0.000 claims description 2
- 238000000034 method Methods 0.000 abstract description 19
- 230000008569 process Effects 0.000 abstract description 13
- 239000000446 fuel Substances 0.000 abstract description 7
- 239000007788 liquid Substances 0.000 abstract description 5
- 230000015572 biosynthetic process Effects 0.000 abstract description 4
- 239000000463 material Substances 0.000 abstract description 3
- 238000005457 optimization Methods 0.000 abstract description 3
- 230000003647 oxidation Effects 0.000 abstract description 3
- 238000007254 oxidation reaction Methods 0.000 abstract description 3
- 238000003786 synthesis reaction Methods 0.000 abstract description 2
- 230000003321 amplification Effects 0.000 abstract 1
- 238000003199 nucleic acid amplification method Methods 0.000 abstract 1
- 238000010248 power generation Methods 0.000 abstract 1
- 238000002407 reforming Methods 0.000 abstract 1
- 239000011269 tar Substances 0.000 description 25
- 238000005516 engineering process Methods 0.000 description 12
- 230000001590 oxidative effect Effects 0.000 description 5
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical group [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 4
- 239000011280 coal tar Substances 0.000 description 4
- 238000011160 research Methods 0.000 description 4
- 239000004071 soot Substances 0.000 description 4
- 230000009471 action Effects 0.000 description 3
- 238000010504 bond cleavage reaction Methods 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 238000011161 development Methods 0.000 description 3
- 230000018109 developmental process Effects 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 230000007017 scission Effects 0.000 description 3
- 239000002023 wood Substances 0.000 description 3
- 229910052799 carbon Inorganic materials 0.000 description 2
- 239000003054 catalyst Substances 0.000 description 2
- 238000007233 catalytic pyrolysis Methods 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 238000001914 filtration Methods 0.000 description 2
- 239000002737 fuel gas Substances 0.000 description 2
- 238000001465 metallisation Methods 0.000 description 2
- 230000001105 regulatory effect Effects 0.000 description 2
- 239000000853 adhesive Substances 0.000 description 1
- 230000001070 adhesive effect Effects 0.000 description 1
- 239000002956 ash Substances 0.000 description 1
- 239000006229 carbon black Substances 0.000 description 1
- 150000001875 compounds Chemical class 0.000 description 1
- 238000005112 continuous flow technique Methods 0.000 description 1
- 230000008878 coupling Effects 0.000 description 1
- 238000010168 coupling process Methods 0.000 description 1
- 238000005859 coupling reaction Methods 0.000 description 1
- 230000009849 deactivation Effects 0.000 description 1
- 230000002950 deficient Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000001035 drying Methods 0.000 description 1
- 230000008030 elimination Effects 0.000 description 1
- 238000003379 elimination reaction Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 238000011065 in-situ storage Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 239000010815 organic waste Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000002035 prolonged effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 230000035484 reaction time Effects 0.000 description 1
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- 238000000629 steam reforming Methods 0.000 description 1
- 230000002194 synthesizing effect Effects 0.000 description 1
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- 239000002699 waste material Substances 0.000 description 1
- 238000005200 wet scrubbing Methods 0.000 description 1
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Images
Classifications
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G1/00—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal
- C10G1/02—Production of liquid hydrocarbon mixtures from oil-shale, oil-sand, or non-melting solid carbonaceous or similar materials, e.g. wood, coal by distillation
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G3/00—Production of liquid hydrocarbon mixtures from oxygen-containing organic materials, e.g. fatty oils, fatty acids
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
- C10J3/485—Entrained flow gasifiers
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/48—Apparatus; Plants
- C10J3/52—Ash-removing devices
- C10J3/526—Ash-removing devices for entrained flow gasifiers
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
- C10J3/64—Processes with decomposition of the distillation products
- C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/10—Feedstock materials
- C10G2300/1011—Biomass
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
- C10G2300/00—Aspects relating to hydrocarbon processing covered by groups C10G1/00 - C10G99/00
- C10G2300/40—Characteristics of the process deviating from typical ways of processing
- C10G2300/4006—Temperature
-
- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/09—Details of the feed, e.g. feeding of spent catalyst, inert gas or halogens
- C10J2300/0913—Carbonaceous raw material
- C10J2300/0916—Biomass
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/10—Process efficiency
- Y02P20/129—Energy recovery, e.g. by cogeneration, H2recovery or pressure recovery turbines
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/141—Feedstock
- Y02P20/145—Feedstock the feedstock being materials of biological origin
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P30/00—Technologies relating to oil refining and petrochemical industry
- Y02P30/20—Technologies relating to oil refining and petrochemical industry using bio-feedstock
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- Chemical & Material Sciences (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Combustion & Propulsion (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Life Sciences & Earth Sciences (AREA)
- Wood Science & Technology (AREA)
- Processing Of Solid Wastes (AREA)
- Industrial Gases (AREA)
Abstract
The invention discloses biomass combined gasification equipment. The equipment comprises a combined gasification furnace, wherein the combined gasification furnace consists of an upper flow section, a transverse flow section and a lower flow section, of which the insides are communicated in turn; the transverse flow section has a square cross section, gases generated by pyrolyzing and gasifying the biomass in the upper flow section of the gasifying furnace tangentially enter the lower flow section of the gasifying furnace together with fine solid particles; the upper flow section is provided with a biomass feed inlet and a primary gasifying agent inlet, the transverse flow section is provided with a secondary gasifying agent inlet, the lower part of the lower flow section is provided with a gas outlet, and the bottom of the lower flow section is an ash separating zone and is provided with an ash outlet. The equipment combines the processes of pyrolysis, gasification, cracking, reforming and partial oxidation in the same reactor to realize zone-based control and optimization of parameters. The equipment has the characteristics of high gasification efficiency, low tar content, high regulation and control capability for gas components, high load adaptability, strong material applicability, stable running and easy amplification, and can be widely applied in the fields of power generation, heat supply, gas supply, liquid fuel synthesis and the like.
Description
Technical field
The present invention relates to the biomass gasification technology field, especially relate to the biomass combined gasification equipment of removing tar in a kind of stove.
Technical background
Because petroleum resources is day by day deficient, environmental pollution and Greenhouse effect problem serious day by day, obtain higher-grade fuel and chemical becomes a kind of development trend just gradually from abundant biomass agriculture and forestry organic waste material resource (as stalk etc.), at home and abroad cause and show great attention to.Biomass gasification technology can become high-grade geseous fuel with various discarded Wood Adhesives from Biomass, is used for industrial generation, cogeneration, central gas supply, industrial heating heat supply, and provides source of the gas etc. as the synthetic gas synthetic liquid fuel and for fuel cell.Biomass gasification process is because technology is flexible, product is of high grade, characteristics such as of many uses, becomes one of the most promising technology of utilizing in the low-grade biomass.Biomass gasification technology has been subjected to extensive attention both at home and abroad, and correlative study has also obtained significant progress.But still there is bottleneck problem in gasification technology at present, when being particularly useful for low-grade biomass, no matter conventional gasification mode all can't be satisfied the demand from aspects such as tar content, gasification efficiency, gas components, therefore, press for the gasifying process that the research tar content is low, combustion gas component ability of regulation and control is strong and easy to operate, solve the bottleneck that exists at present, the biogas metallization processes is made breakthroughs, highlight its superiority in new Application Areas.
At different industrial uses, biomass gasification technology has been carried out a large amount of research and developments both at home and abroad, develop different biogas metallization processes such as fixed bed, fluidized-bed, air flow bed.No matter adopt which kind of gasifying process, the generation of tar is the common problem of gasification technology.Tar is gaseous state when high temperature, mix fully with inflammable gas, and be condensed into liquid state when low temperature, and its separation and processing be difficulty very.The existence of tar has not only reduced gasification efficiency, gas heating value, and more seriously tar is condensed into liquid state when low temperature, and easily and combinations such as water, coke, ash, the obstruction gas pipe line influences the normal operation of equipment for gasification; The tar that is condensed into fine drop is difficult to burn, and is easy to generate particles such as carbon black when burning, and gas-fired equipment is caused great infringement.The existence of tar greatly reduces the utility value of synthetic gas, has stoped the high-end applications of gasification technology, is the bottleneck problem of the efficient large-scale application of gasification technology.
Industrial tar removal method commonly used mainly is that stove is removed outward at present, as dry type filtration, wet scrubbing, catalytic pyrolysis etc.Though filtration and method for washing are simple to operate, cost is lower, efficient is not high, for preventing secondary pollution, need to increase extra treating plant and sewage treatment equipment, not only occupation of land is bigger, has also increased cost of investment, and the tar of disposing can not utilize, and causes the waste of the energy.The catalytic pyrolysis system is simple, capacity usage ratio is high, and the biological fuel gas component is had promotor action and becomes the focus of domestic and international research, but needs to consume a large amount of additional energies, also needs extra utility appliance, has increased complicacy and the investment of system.Simultaneously, because problems such as catalyst deactivation, mechanical wear and application cost are mainly used in experimental study at present, also do not form business-like special-purpose catalyst series, especially also have bigger distance from commercialization aspect the work-ing life of catalyzer.
Tar also can suppress in vapourizing furnace namely that tar produces and is target product gas with the tar converted in-situ that produces by the method removed in the stove, realizes not containing tar in the crude synthesis gas in the vapourizing furnace.Remove in the stove and can realize by optimizing methods such as adding catalyzer in gasification furnace structure design, optimization gasification operating parameters, the vapourizing furnace, reduce the purpose that vapourizing furnace exports the coal-tar middle oil content of combustion gas thereby reach.This method is focus and the Future Development direction of research at present.
Both at home and abroad the development trend of gasification technology be that exploitation is efficient, low tar, gasifying process that combustion gas component ability of regulation and control is stronger.At the effective elimination of tar and the high-end utilization of combustion gas, carried out the research of novel gasifying process both at home and abroad.As: Technical University Of Denmark has designed two-stage gasifier, and the coal-tar middle oil content of gained combustion gas reduces greatly; Germany Choren company has proposed the technology of mild pyrolysis and high temperature pyrolysis two-step method making high quality synthetic gas, contains tar in the synthetic gas hardly.These apparatus features be with many reactors in series on a continuous flow process, fuel drying and pyrolysis in the indirect heating type cracker earlier, the product of the cracking and then lane between cracker and coke gasification device carries out partial oxidation, product gas flow is through the coke bed of heat, thereby makes the coke tar cracking in the product gas and reach lower content.
Therefore, mostly the gasifying process that removes tar at present in the stove is to utilize the series connection of several reactors to realize, having only publication number is that the Chinese patent of " CN101225315A " has proposed integrated biomass combined gasification equipment, but owing to be subjected to the restriction of structure space, the particle residence time is short, secondary reaction is insufficient in the stove, and the component modulation is indifferent.
Summary of the invention
The invention provides a kind of biomass combined gasification equipment, can be with reacting phases such as pyrolysis, burning, gasification, coke tar cracking, reformation and component regulation and control to separating, realize the control of parameter subregion and optimize coupling, all processes are finished in a covering device simultaneously, even do not use catalyzer also can reach the purpose that reduces tar content, adjustments of gas component.
For reaching above purpose, the present invention has taked following technical scheme:
Apparatus of the present invention comprise composite gasification furnace, and the vapourizing furnace upper flow section that described composite gasification furnace is communicated with successively by inside, vapourizing furnace crossing current section and vapourizing furnace are formed for dirty section.Be provided with biomass feed inlet and a gasification agent inlet in described vapourizing furnace upper flow section; Vapourizing furnace crossing current section is provided with second gasification agent entrance; The bottom that vapourizing furnace is dirty section is provided with gas outlet, and dirty section bottom of vapourizing furnace is the ash separation district, is provided with the ash content outlet.
Described vapourizing furnace upper flow section can be identical with dirty section diameter, and dirty section height be more than or equal to 2/3 of upper flow section height, and the fluid flow direction in upper flow section and dirty section is opposite, and the ratio of upper flow section sectional area and crossing current section sectional area is greater than 10.
A described gasification agent inlet can be arranged on the bottom of vapourizing furnace upper flow section, makes vaporized chemical enter vapourizing furnace by the bottom of vapourizing furnace upper flow section.
A described vaporized chemical and second gasification agent are air or oxygen or oxygen-rich air, and can be according to the water vapour of reaction needed adding.Described vapourizing furnace upper flow section and dirty section are the circular section, the crossing current section is the square-section, upper flow section tangentially is connected by the crossing current section with dirty section, and the combustion gas that biomass produce at vapourizing furnace upper flow section pyrolytic gasification is carried the tiny solid particle secretly and tangentially entered dirty section of vapourizing furnace through vapourizing furnace crossing current section.Because oxidizing reaction takes place in the crossing current section in part combustion gas and second gasification agent, temperature raises rapidly, volume expands rapidly, and the ratio of upper flow section sectional area and crossing current section sectional area is greater than 10, so crossing current section flow velocity can reach more than 10 times of upper flow section flow velocity, form high speed whirlwind when combustion gas tangentially enters dirty section, be conducive to combustion gas mixing and solid soot particle and separate, prolonged coke tar cracking, reformation, the secondary reaction time of dirty section of vapourizing furnace simultaneously.
Pyrolysis, gasification and biomass coke partial combustion reaction take place in biomass in the vapourizing furnace upper flow section, in vapourizing furnace crossing current section the biological fuel gas partial combustion takes place and react, and in dirty section of vapourizing furnace coke tar cracking, reformation, secondary reaction take place.
In this device, the vapourizing furnace upper flow section is as the biomass pyrogenation gasification district, and temperature is 500-900 ℃, wherein the vapourizing furnace upper flow section in, top form biomass pyrolysis district, temperature is 500-700 ℃, and the bottom of vapourizing furnace upper flow section is biomass coke gasification and partial combustion district, temperature 800-900 ℃; Vapourizing furnace is the high-temperature zone as coke tar cracking, reformation, secondary reaction district for dirty section, and temperature can reach 1000-1300 ℃; The gas outlet pipe of the dirty pars infrasegmentalis gas outlet of vapourizing furnace can stretch into the position of dirty section circular section diameter of about 1/4-1/2 vapourizing furnace in dirty section, prevent from entering the gas outlet pipe along the solid soot particle that dirty section wall backspin separates, dirty section bottom is the ash separation district, is provided with the ash content outlet.By adding different vaporized chemicals, the temperature of same district not in the control stove, the component of regulating combustion gas realizes control and the optimization of different operating modes in a stove.
Biomass combined gasification equipment of the present invention is compound in same reactor with pyrolysis, gasification, cracking, reformation, partial oxidation process, realizes the control of parameter subregion and optimizes.The characteristics that this device has the gasification efficiency height, tar content is low, the gaseous fraction ability of regulation and control is strong, load performance strong, the raw material suitability is strong, stable, be easy to amplify.This device is used for tar content≤20mg/Nm that gasifying biomass can make combustion gas
3, and stable, continuous, can be applicable to multiple field, as generating, heat supply, air feed, synthetic liquid fuel etc.
Description of drawings
Fig. 1 is apparatus of the present invention example structure synoptic diagram (front view);
Fig. 2 is the plan structure synoptic diagram of Fig. 1.
Description of reference numerals:
1. 6. gasification agent inlet 7. vapourizing furnaces in dirty section 3. biomass feed inlet 4. biomass pyrolytic districts, 5. coke gasifications of vapourizing furnace upper flow section 2. vapourizing furnaces and partial combustion district crossing current section, 8. second gasification agent entrances, 9. ash separation districts, 10. gas outlets
Embodiment
Below in conjunction with accompanying drawing and embodiment content of the present invention is described further.
As shown in Figure 1, 2, apparatus of the present invention comprise composite gasification furnace, and the vapourizing furnace upper flow section 1 that described composite gasification furnace is communicated with successively by inside, vapourizing furnace crossing current section 7 and vapourizing furnace are formed for dirty section 2.Be provided with biomass feed inlet 3 in vapourizing furnace upper flow section 1, the bottom is provided with gasification agent inlet 6 one time; In the vapourizing furnace upper flow section 1, top form biomass pyrolysis district 4, the bottom is coke gasification and partial combustion district 5.Vapourizing furnace upper flow section and dirty section are the circular section, the diameter that vapourizing furnace upper flow section 1 and vapourizing furnace are dirty section 2 can be identical, dirty section height is more than or equal to 2/3 of upper flow section height, vapourizing furnace crossing current section 7 is the square-section, the ratio of the sectional area of the sectional area of upper flow section 1 and crossing current section 7 is greater than 10, and the combustion gas that biomass produce at vapourizing furnace upper flow section 1 pyrolytic gasification is carried the tiny solid particle secretly and tangentially entered dirty section 2 of vapourizing furnace through vapourizing furnace crossing current section 7.Be provided with second gasification agent entrance 8 at described vapourizing furnace crossing current section 7 entrances.The bottom that vapourizing furnace is dirty section 2 is provided with gas outlet 10, and the gas outlet pipe stretches into the position of dirty section circular section diameter of about 1/4-1/2 vapourizing furnace in dirty section, and the bottom is ash separation district 9, is provided with the ash content outlet.
Embodiment 1:
Pyrolytic reaction takes place from the pyrolysis zone 4 that opening for feed 3 adds in the composite gasification furnace upper flow section 1 in the biomass wood chip under 500-700 ℃ of temperature, biomass discharge volatilization gas, and generates solid coke; The coke macrobead flows into coke gasification and the partial combustion district 5 in the vapourizing furnace upper flow section 1 downwards, at the oxygen-rich air (O of gasification agent inlet 6 addings
2Concentration 90%) under the effect, small part coke generation oxidizing reaction makes coke gasification and partial combustion district 5 temperature reach 800-900 ℃, and most of coke then generating gasification reaction generates inflammable gas; The 5 high-temperature gas form biomass pyrolysis districts 4 of upwards flowing provide biomass pyrolytic required heat from coke gasification and partial combustion district, keep the temperature of pyrolysis zone 4 at 500-700 ℃; Biomass at gas entrainment tiny solid particle that vapourizing furnace upper flow section 1 internal reaction produces in vapourizing furnace crossing current section 7 tangentially enters dirty section 2 of vapourizing furnace.Add an amount of secondary oxygen-rich air from second gasification agent inlet mouth 8, make part inflammable gas generation oxidizing reaction, temperature raises rapidly, volume expands rapidly, and since the ratio of the sectional area of the sectional area of upper flow section 1 and crossing current section 7 greater than 10, so the flow velocity of crossing current section 7 can reach more than 10 times of flow velocity of upper flow section 1, combustion gas tangentially enters dirty section 2 o'clock formation high speed whirlwind.Dirty section 2 interior local temperature of vapourizing furnace can reach about 1200 ℃, and tar scission reaction takes place under this hot conditions changes into inflammable gas, and the carbon residue in the particle that combustion gas is simultaneously carried secretly also can change into inflammable gas by secondary reaction; Enter in the process of dirty section 2 of vapourizing furnace at the tangential high speed rotating of combustion gas, the solid soot particle that it carries is separated the ash separation district 9 that the bottom of dirty section 2 of downward inflow vapourizing furnace connects from gas under centrifugal action, inflammable gas then enters downstream unit from the gas outlet 10 of dirty section 2 bottoms of vapourizing furnace.During oxygen-rich air equivalence ratio ER=0.21-0.29, the gas component that obtains is H
221.4%-25.4%, N
22.9%-3.8%, CO 38.8%-45.2%, CH
44.9%-7.0%, CO
218.5%-25.1%, gasification efficiency 74.9%-85.0%, efficiency of carbon conversion 91.8%-99.6%.Do not feed under the situation of secondary oxygen-rich air vaporized chemical in dirty section 2 of vapourizing furnace, the coal-tar middle oil content of gas outlet 10 inflammable gass is 900mg/m
3When feeding secondary oxygen-rich air vaporized chemical, scission reaction takes place in the high-temperature zone in tar, and the coal-tar middle oil content of the inflammable gas of gas outlet 10 is down to 20mg/m
3Below.Behind the coke tar cracking in the combustion gas each components contents do not have considerable change because coke tar cracking is except N
2Outer other gases have generation, but coke tar cracking becomes inflammable gas to make the biomass gas generating rate by 1.07Nm
3/ kg brings up to 1.21Nm
3/ kg.
Embodiment 2:
Pyrolytic reaction takes place from the pyrolysis zone 4 that opening for feed 3 adds in the composite gasification furnace upper flow section 1 in the biomass wood chip under 500-700 ℃ of temperature, biomass discharge volatilization gas, and generates solid coke; The coke macrobead flows into coke gasification and the partial combustion district 5 in the vapourizing furnace upper flow section 1 downwards, at the oxygen-rich air (O from gasification agent inlet 6 addings
2Concentration 90%) under the effect, small part coke generation oxidizing reaction makes coke gasification and partial combustion district 5 temperature reach 800-900 ℃, and most of coke then generating gasification reaction generates inflammable gas; The 5 high-temperature gas form biomass pyrolysis districts 4 of upwards flowing provide biomass pyrolytic required heat from coke gasification and partial combustion district, keep the temperature of pyrolysis zone 4 at 500-700 ℃; Biomass at gas entrainment tiny solid particle that vapourizing furnace upper flow section 1 internal reaction produces in vapourizing furnace crossing current section 7 tangentially enters dirty section 2 of vapourizing furnace.Add an amount of secondary oxygen-rich air from second gasification agent inlet mouth 8, make part inflammable gas generation oxidizing reaction, temperature raises rapidly, volume expands rapidly, and since the ratio of the sectional area of the sectional area of upper flow section 1 and crossing current section 7 greater than 10, so the flow velocity of crossing current section 7 can reach more than 10 times of flow velocity of upper flow section 1, combustion gas tangentially enters dirty section 2 o'clock formation high speed whirlwind.For improving H in gas outlet 10 inflammable gass
2/ CO ratio namely improves H
2Content reduces CO content, improves the synthetic gas quality, adds water steam in the second gasification agent, by water gas shift reaction CO+H
2O → CO
2+ H
2And steam reforming reaction, gaseous fraction is regulated and control.Local temperature under second gasification agent reaction conditions in dirty section 2 of the vapourizing furnace can reach about 1100 ℃, and tar scission reaction takes place under this hot conditions changes into inflammable gas, and water gas shift reation makes the H in the combustion gas
2Be subjected to directed regulation and control with the CO component; Carbon residue in the grain that combustion gas is simultaneously carried secretly also can change into inflammable gas by secondary reaction; Enter in the process of dirty section 2 of vapourizing furnace at the tangential high speed rotating of combustion gas, the solid soot particle that it carries is separated the ash separation district 9 that the bottom of dirty section 2 of downward inflow vapourizing furnace connects from gas under centrifugal action, inflammable gas then enters downstream unit from the gas outlet 10 of dirty section 2 bottoms of vapourizing furnace.Under oxygen-rich air equivalence ratio ER=0.26 situation, when water vapour/biomass material during than (quality) S/B=0.1-0.5, the gas component that obtains is H
224.6%-28.7%, N
22.8%-3.8%, CO 27.1%-33.8%, CH
43.9%-4.1%, CO
229.3%-32.7%, gasification efficiency 73.9%-78%, efficiency of carbon conversion 97.5%-98.4%.With embodiment 1 more as can be known, make H by adding water vapour
2/ CO mean value brings up to 0.88 by 0.56, and the highest having reached more than 1.0 is conducive to follow-up building-up reactions and uses, but CO
2Content increases, and needs to remove before synthesizing.
Claims (4)
1. biomass combined gasification equipment, comprise composite gasification furnace, it is characterized in that: the vapourizing furnace upper flow section that described composite gasification furnace is communicated with successively by inside, vapourizing furnace crossing current section and vapourizing furnace are formed for dirty section, described vapourizing furnace upper flow section is identical with the diameter of dirty section of vapourizing furnace, and dirty section height is more than or equal to 2/3 of upper flow section height; The ratio of described upper flow section sectional area and crossing current section sectional area is greater than 10; Be provided with biomass feed inlet and a gasification agent inlet in described vapourizing furnace upper flow section; Vapourizing furnace crossing current section is provided with second gasification agent entrance, and described second gasification agent entrance is arranged on crossing current section entrance; The bottom that vapourizing furnace is dirty section is provided with gas outlet, and dirty section bottom of vapourizing furnace is the ash separation district, is provided with the ash content outlet; Described vapourizing furnace upper flow section is as the biomass pyrogenation gasification district, temperature is 500-900 ℃, wherein the vapourizing furnace upper flow section in, top form biomass pyrolysis district, temperature is 500-700 ℃, the bottom of vapourizing furnace upper flow section is biomass coke gasification and partial combustion district, temperature 800-900 ℃; Dirty section of vapourizing furnace is as coke tar cracking, reformation, secondary reaction district, and temperature can reach 1000-1300 ℃; Described vapourizing furnace upper flow section and dirty section are the circular section, the crossing current section is the square-section, upper flow section tangentially is connected by the crossing current section with dirty section, and the combustion gas that biomass produce at vapourizing furnace upper flow section pyrolytic gasification is carried the tiny solid particle secretly and tangentially entered dirty section of vapourizing furnace through vapourizing furnace crossing current section.
2. biomass combined gasification equipment as claimed in claim 1 is characterized in that, described gas outlet pipe stretches into the position of dirty section circular section diameter of 1/4-1/2 vapourizing furnace in dirty section of the vapourizing furnace.
3. biomass combined gasification equipment as claimed in claim 1 is characterized in that, a described vaporized chemical and second gasification agent are air or oxygen or oxygen-rich air.
4. biomass combined gasification equipment as claimed in claim 3 is characterized in that, can add water vapour according to reaction needed in a described vaporized chemical and the second gasification agent.
Priority Applications (2)
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|---|---|---|---|
| CN2010101879126A CN101845328B (en) | 2010-05-24 | 2010-05-24 | Biomass combined gasification equipment |
| PCT/CN2010/080215 WO2011147180A1 (en) | 2010-05-24 | 2010-12-24 | Biomass combined gasification equipment |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN2010101879126A CN101845328B (en) | 2010-05-24 | 2010-05-24 | Biomass combined gasification equipment |
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| CN101845328B true CN101845328B (en) | 2013-08-28 |
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| CN101845328B (en) * | 2010-05-24 | 2013-08-28 | 中国科学院广州能源研究所 | Biomass combined gasification equipment |
| CN102154044B (en) * | 2011-03-11 | 2013-10-30 | 周鼎力 | Method for preparing engine fuel gas by using biomass and/or organic waste |
| JP6369161B2 (en) * | 2013-12-13 | 2018-08-08 | 株式会社Ihi | Tar reforming furnace |
| CN108998099B (en) * | 2018-08-20 | 2020-08-04 | 浙江大学 | Gasification method for household garbage with staggered grates |
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| CN101225315A (en) * | 2007-12-18 | 2008-07-23 | 中国科学院广州能源研究所 | Method and device for biomass compound gasification |
| CN201459073U (en) * | 2009-09-04 | 2010-05-12 | 刘黎黎 | Biomass catalytic gasification furnace |
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| WO2002051966A1 (en) * | 2000-12-26 | 2002-07-04 | Ebara Corporation | Fluidized-bed gasification method and apparatus |
| CN101613625B (en) * | 2009-06-18 | 2012-10-10 | 扬州工业职业技术学院 | Method and device for detarring small-sized biomass gasifier |
| CN201501850U (en) * | 2009-09-16 | 2010-06-09 | 北京乡电电力有限公司 | Biomass gasifier provided with tar catalytic cracking unit |
| CN201713504U (en) * | 2010-05-24 | 2011-01-19 | 中国科学院广州能源研究所 | Biomass composite gasification device |
| CN101845328B (en) * | 2010-05-24 | 2013-08-28 | 中国科学院广州能源研究所 | Biomass combined gasification equipment |
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| CN101225315A (en) * | 2007-12-18 | 2008-07-23 | 中国科学院广州能源研究所 | Method and device for biomass compound gasification |
| CN201459073U (en) * | 2009-09-04 | 2010-05-12 | 刘黎黎 | Biomass catalytic gasification furnace |
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